Distributor device for a multiple-bed downflow reactor

ABSTRACT

The invention relates to a device and method for distributing a liquid and gas in a multiple-bed downflow reactor, such as a hydrocarbon processing reactor, like a hydrocracker. The device comprises respectively the method uses a distributor device comprising a substantially horizontal collecting tray provided with a central gas passage. Gas passing in downward direction through the central gas passage is forced into a swirling motion by a swirler. This swirling motion has a swirl direction around a vertical swirl axis so that the gas leaves the central gas passage as a swirl. At a location above the collecting tray, a quench fluid is ejected into gas in an ejection direction, which is, viewed in a horizontal plane, at least partly opposite to the swirl direction.

PRIORITY CLAIM

The present application is the National Stage (§371) of InternationalApplication No. PCT/EP2012/076438, filed Dec. 20, 2012, which claimspriority from International application No. PCT/US2011/066923, filedDec. 22, 2011 the disclosures of which are incorporated herein byreference.

The present invention relates to a distributor device for a multiple-beddownflow reactor, a multiple-bed downflow reactor comprising such adistributor device, use of such a distributor device and reactor,respectively, in hydrocarbon processing and a distributing method fordistributing liquid and gas in a multiple-bed downflow reactor.

Multiple-bed downflow reactors containing a number of superimposedreaction beds are used in the chemical and petroleum refining industriesfor affecting various processes such as catalytic dewaxing,hydrotreating and hydrocracking. In these processes a liquid phase istypically mixed with a gas phase and the fluids pass over a particulatecatalyst maintained in the reaction beds. As the fluids passconcurrently through a reaction bed, the distribution of liquid and gasacross the reaction bed will tend to become uneven with adverseconsequences with regard to the extent of reaction and also temperaturedistribution. In order to achieve a uniform distribution of liquid andgas and of temperature in the fluids entering the next lower reactionbed, a fluid distributor device, of which there are many differenttypes, is usually placed between the reaction beds.

Such a fluid distributor device is known from EP-A-716881. This devicediscloses a fluid distributor device for use between the reaction bedsof a multiple-bed downflow reactor. This known device comprises:

a substantially horizontal collecting tray provided with:

-   -   a central gas passage and    -   liquid passages around the central gas passage;

a swirler, which swirler:

-   -   is located above the collecting tray around the central gas        passage, and    -   is provided with vanes defining a swirl direction and being        arranged to impart a swirling motion to gas passing through the        central gas passage so that the gas leaves the central gas        passage as a swirl swirling in said swirl direction around a        vertical swirl axis;

one or more ejection nozzles located above the collecting tray andarranged for ejecting, in an ejecting direction, a quench fluid into thegas before said gas enters the swirler.

During normal operation, liquid descending from the upper reaction bedcollects on the collecting tray where it accumulates to form a layer ofliquid that covers the liquid passages so that flow of gas through themis precluded. The flow of gas into a lower portion of the reactor ispassed through the swirler located on the collecting tray above andaround the central gas passage and subsequently through the centralpassage. On entering the swirler, vanes impart a swirling motion to thegas which is only able to move downwardly through the central gaspassage into the mixing chamber below the collecting tray. The swirldirection of the swirl motion of the gas is defined by the vanes of theswirler and is around an essentially vertical swirl axis. The swirlingmotion of the gas promotes gas-gas interactions and thus equilibrationof the gas phase. Liquid collected on the collecting tray passes throughthe liquid passages into the guide conduits. The guide conduits haveinjection nozzles injecting the liquid into the swirl of gas coming fromthe central gas passage. This liquid injected into the swirl leaves theinjection nozzles in an injection direction.

In order to achieve a uniform distribution of liquid and gas and oftemperature in the fluids entering the next lower reaction bed, a fluiddistributor device, like the one of EP-A-716881 is frequently providedwith one or more ejection nozzles to eject a quench fluid into the gasbefore it enters the swirler. For this purpose one of the embodiments ofEP-A-716881 has a quench ring arranged above the collecting tray. Theinner side of this quench ring is provided with a plurality of ejectionnozzles. In use a quench fluid is ejected into the gas passing from theupper bed to the swirler. EP-A-716881 is silent about the ejectiondirection of the ejection nozzles. It can only be seen in the drawingthat these ejection nozzles are arranged on the inner side of the quenchring and face in an inward direction of the quench ring. However, frompractise it is known that, in order to prevent a pressure drop andconsequently loss of energy, these ejection nozzles are directed in ahorizontal plane, that the ejection direction is at an angle withrespect to the radial extending between the ejection nozzle and thecentre of the reactor such that the ejection direction is (partly) inthe same direction as the swirl direction of the swirl imparted by theswirler.

The ejection direction of EP-A-716881—as well as the ejection directionof the present invention—can mathematically be represented by an arrow,called ejection vector. In turn this ejection vector of EP-A-716881—aswell as the one of the present invention—can be represented by anorthogonal set of three vector components: a radial ejection vectorextending perpendicular to the swirl axis, an axial ejection vectorextending parallel to the swirl axis and a tangential ejection vectorextending tangentially with respect to the swirl axis. Taking intoaccount this representation, the ejection direction of EP-A-716881 asknown from practise—as described in the preceding paragraph—can berepresented as follows: axial ejection vector has a length zero (meaningit is absent) as the ejection is in horizontal direction; the radialejection vector is, viewed from the ejection nozzle, directed towardsthe centre of the reactor (which corresponds to the swirl axis); and thetangential ejection vector is, viewed from the ejection nozzle, directedin the same direction as the swirl direction.

The object of the invention is to provide an improved distributor deviceaccording to the preamble of claim 1.

This object is according to a first aspect of the invention achieved byproviding a distributor device for distributing liquid and gas in amultiple-bed downflow reactor;

wherein the distributor device comprises:

a substantially horizontal collecting tray provided with:

-   -   a central gas passage and    -   liquid passages around the central gas passage;

a swirler, which swirler:

-   -   is located above the collecting tray around the central gas        passage, and    -   is provided with vanes defining a swirl direction and being        arranged to impart a swirling motion to gas passing through the        central gas passage so that the gas leaves the central gas        passage as a swirl swirling in said swirl direction around a        vertical swirl axis;

one or more ejection nozzles located above the collecting tray andarranged for ejecting, in a ejecting direction, a quench fluid into thegas before said gas enters the swirler;

wherein the ejection direction is represented in an orthogonal set ofthree ejection vectors comprised of a radial ejection vector extendingperpendicular to the swirl axis, an axial ejection vector extendingparallel to the swirl axis and a tangential ejection vector extendingtangentially with respect to the swirl axis; and

wherein the ejection nozzle is directed such that the tangentialejection vector of the ejection direction of the ejected quench fluid isdirected opposite to the swirl direction. As the tangential ejectionvector is directed in a direction, it is represented by an arrow havinga length larger than zero (i.e. the tangential ejection vector is largerthan zero).

The tangential ejection vector being directed opposite to the swirldirection, means that the ejection direction is, viewed in a horizontalplane, at least partly counterflow to the swirl direction. Due to theejection direction being partly opposite the swirl direction, a pressuredrop and loss of energy will occur. The expected result would thereforebe a decrease of the performance of the reactor provided with theinvented distributor device. However, experiments showed the opposite.

The performance of a first reactor provided with a first distributordevice according to EP-A-716881—having, as known from practise, theejection direction in a horizontal plane at such an angle with respectto the radial that the radial ejection vector is directed towards thecentre of the reactor and the tangential ejection vector directed in thesame direction as the swirl direction—was compared with the performanceof the same first reactor provided with a second distributor devicewhich was, except for the direction of the ejection nozzles, the same asthe first distributor device. The quench fluid was in both cases ahydrogen gas having a temperature lower than the temperature of thefluid into which it is ejected. Comparative computational model studiesrevealed, that, at the (horizontal) level where the fluid enters intothe bed following the distributor device, applying the inventionresults, viewed in a horizontal plane, in a 50% reduction of thestandard deviation of fluid temperature across the catalyst bed. Thisstandard deviation is in this application also called the ‘exit standarddeviation’. Reduction of this standard deviation reduces the catalystdeactivation and makes it possible for the reactor to continue longer inoperation. Taking into account that extension of the operation with oneday can be equivalent to an increase in profit of about one millioneuro, reduction of this standard deviation is of very significantimportance.

With respect to the ejection nozzle, it is noted that during normal use,the stream of fluid emerging from a ejection nozzle will, according tothe invention, in general be a gas stream, but it is according to theinvention not excluded that the stream is a mixture of a liquid and agas. In the field of hydrocarbon processing, the quench fluid is ingeneral gaseous hydrogen optionally comprising light carbons as anadditive. Further, with respect to the ejection nozzle, it is noted thatthe stream emerging from this nozzle in said ejection direction can be ajet-shaped, fan-shaped, cone-shaped, etcetera. The ejection directionwill be the main direction.

According to a further embodiment of the distributor device according toaccording to the first aspect of the invention, the ejection nozzle isdirected such that the radial ejection vector of the ejection directionis directed to the swirl axis. As the radial ejection vector is in thisembodiment directed in a direction, it is represented by an arrow havinga length larger than zero (i.e. the radial ejection vector is largerthan zero). The radial ejection vector being directed towards the swirlaxis, means that the ejection direction is, viewed in a horizontalplane, not fully, but partly, in counterflow to the swirl direction.This improves the homogeneity of the temperature across the swirl,assumably because the ejected quench fluid is better capable of reachingthe centre of the swirl.

Simulative calculations show, that reduction of the so called ‘exitstandard deviation’ is obtained already when the ejection direction andassociated radial injection vector of a said injection nozzle define anangle of more than 2.5°, such as at least 5°, and that this reductionbecomes considerable when this angle is at least 7.5°, such as at least10°. Simulative calculations further show that the effect of thereduction of said ‘exit standard deviation’ appears to disappear whenthis angle becomes larger than 35°, and that the considerable reductionof said ‘exit standard deviation’ appears to diminish when this anglebecomes larger than 30°.

According to a further embodiment of the distributor device according tothe first aspect of the invention, the ejection direction and associatedradial ejection vector of a said ejection nozzle consequently define anangle in the range of [5°, 35°], such as in the range of [7.5°, 30°] orin the range of [7.5°, 25°], like in the range of [15°, 25°]. It isnoted here that, throughout this application, the indications ‘[’and‘]’mean that the respective value is included in the range, and theindication ‘,’ ‘up to’.

With respect to the angles between the ejection direction and associatedradial ejection vector, it is noted that these are expressed in degrees,wherein 360° corresponds with a circle.

According to a further embodiment of the distributor device according tothe first aspect of the invention, the distributor device furthercomprises a mixing chamber defined between the collecting tray and thedistribution tray.

According to a further embodiment of the distributor device according tothe first aspect of the invention, the central gas passage is surroundedby a weir. This weir prevents liquid from entering into the gas passage.

According to a further embodiment of the distributor device according tothe first aspect of the invention, the distributor device furthercomprises a cover located above the central gas passage and covering theentire central gas passage. This cover prevents fluid from approachingthe central gas passage in a vertical downward direction.

According to a further embodiment of the distributor device according tothe first aspect of the invention, the distributor device comprises oneor more guide conduits arranged below the collecting tray, wherein theguide conduits have first ends communicating with the liquid passages ofthe collecting tray for receiving liquid; and second ends provided witha injection nozzle arranged to inject, in an injection direction, liquidreceived by the first ends into the swirl. Like the ejection directionof the ejection nozzles, also the injection direction of the injectionnozzles can be defined as an orthogonal set of three injection vectorscomprised of a radial injection vector extending perpendicular to theswirl axis, an axial injection vector extending parallel to the swirlaxis and a tangential injection vector extending tangentially withrespect to the swirl axis.

With respect to the terms ‘injection’ and ‘ejection’ as used in thisapplication, it is noted that these are not intended to have physicallya different meaning, these different terms are only intended todifferentiate between what is associated to the swirl (the term‘injection’) and quench (the term ‘ejection’). Further, with respect tothe injection nozzle, it is noted that the stream emerging from thisnozzle in said injection direction can be a jet-shaped, fan-shaped,cone-shaped, etcetera. The injection direction will be the maindirection.

According to a further embodiment of the distributor device according tothe first aspect of the invention, the distributor device furthercomprises a substantially horizontal pre-distribution tray arrangedbelow the central gas passage, above the distribution tray, and, in casepresent, lower than the optional injection nozzles of the one or moreguide conduits, which pre-distribution tray is provided with an overflowweir at its perimeter and a plurality of openings near the perimeter.

According to a further embodiment of the distributor device accordingthe first aspect of to the invention, the one or more guide conduitscomprise at least eight guide conduits distributed around the centralgas passage.

According to a further embodiment of the distributor device accordingthe first aspect of to the invention, the injection nozzles of the oneor more guide conduits are arranged to lie within the same horizontalplane

According to a further embodiment of the distributor device according tothe invention, the one or more ejection nozzles comprise a plurality ofnozzles arranged around the swirl axis to lie within the same horizontalplane.

According to a further embodiment of the distributor device accordingthe first aspect of the invention, the distributor device furthercomprises a substantially horizontal distribution tray located below thecollecting tray, which distribution tray is provided with a plurality ofdowncomers for downward flow of liquid and gas; each downcomeroptionally comprising an upstanding, open ended tube having an apertureat its side for entry of liquid into the tube.

According to a further embodiment of the distributor device accordingthe first aspect of to the invention, the ejection nozzles are arrangedto lie within the same horizontal plane. This same horizontal plane canaccording to an additional embodiment lie, viewed in vertical direction,at the same level as the vanes.

According to a second aspect, the invention also relates to amultiple-bed downflow reactor comprising vertically spaced beds of solidcontact material, e.g. a catalyst, and a distributor device positionedbetween adjacent beds, wherein the distributor device is according tothe first aspect of this invention.

According to a third aspect, the invention relates to the use of adistributor device according to the first aspect of the invention inhydrocarbon processing, such as in a hydrotreating and/or hydrocrackingprocess.

According to a fourth aspect, the invention relates to the use of adownflow reactor according to the second aspect in hydrocarbonprocessing, such as in a hydrotreating and/or hydrocracking process.

According to a fifth aspect, the invention relates to a distributingmethod for distributing liquid and gas in a multiple-bed downflowreactor, such as a hydrocarbon processing reactor, like a hydrocracker;

wherein a distributor device is used, which distributor device comprisesa substantially horizontal collecting tray provided with a central gaspassage;

wherein gas passing in downward direction through the central gaspassage is forced into a swirling motion having a swirl direction arounda vertical swirl axis so that the gas leaves the central gas passage asa swirl;

wherein liquid is collected on the collecting tray;

wherein, at a location above the collecting tray and before the gasenters the swirler, a quench fluid, like a gaseous quench fluid, isejected into said gas in an ejection direction, which is, viewed in ahorizontal plane, at least partly opposite to the swirl direction.

According to a further embodiment of the fifth aspect, the ejectiondirection is represented in an orthogonal set of three ejection vectorscomprised of a radial ejection vector extending perpendicular to theswirl axis, an axial ejection vector extending parallel to the swirlaxis and a tangential ejection vector extending tangentially withrespect to the swirl axis; wherein the tangential ejection vector isdirected opposite to the swirl direction. In this embodiment, the radialejection vector may be directed to the swirl axis. According to still afurther embodiment of the fifth aspect, the ejection direction andassociated radial ejection vector define an angle in the range of [5°,35°], such as in the range of [7.5°, 30°], like in the range of [7.5°,25°] or in the range of [15°, 25°].

The invention will now be further described by way of example withreference to the accompanying drawings in which:

FIG. 1 shows schematically a vertical cross-section of a portion of amultiple bed downflow reactor with a distributor device according to theinvention;

FIG. 2 shows schematically a 3-dimensional representation of a vectordefined by a set of three orthogonal vector components; and

FIG. 3 shows a view, according to arrows III in FIG. 1, onto thecollecting tray 20.

In the drawings like parts are denoted by like reference numerals.

FIG. 1 shows a cross-sectional view through the portion of a multiplebed downflow reactor in the region between an upper bed 15 and a lowerbed 115. This region between the upper bed 15 and lower bed 115 isprovided with a distributor device 2. The general configuration of thereactor will be conventional and details such as supports for thedistribution tray are not shown for purposes of clarity.

In this embodiment, the wall 5 of the reactor 1 and the support grid 10support an upper reaction bed 15 of solid contact material, e.g.catalyst, in particulate form, over which catalyst reactants flow andare at least partially converted into product. The support grid 10 isprovided with passages (not shown) and may be of conventional type.Catalyst may be directly arranged on the support grid 10 or the catalystmay be arranged on a layer of support balls (not shown) which permitliquid and gas to flow downwardly out of the upper bed 15 and throughthe support grid 10, which support balls are arranged on the supportgrid 10.

The distributor device 2 comprises a substantially horizontal collectingtray 20 supported on a ledge 25 which is provided with a central gaspassage 30 surrounded by a weir 35 and with liquid passages 40 aroundthe weir 35. A substantially horizontal distribution tray 45 locatedbelow the collecting tray 20. The distribution tray 45 is provided witha plurality of tubular downcomers 50 for downward flow of liquid andgas. A cover 55 is located above the central gas passage 30 of thecollecting tray 20 and covers the entire central gas passage, so thatgas coming from the upper bed 15 is prevented from axially approachingthe central gas passage 30. A mixing chamber 60 is defined between thecollecting tray 20 and the distribution tray 45. Guide conduits 65having first ends 70 and second ends 76 are arranged below thecollecting tray 20. The first ends 70 of the guide conduits 65communicate with the liquid passages 40 of the collecting tray 20 inorder to receive liquid collected by the collecting tray 20. Each secondends 76 is provided with an injection nozzle 75 opening into the mixingchamber 60.

The distributor device 2 further comprises a substantially horizontalpre-distribution tray 80 arranged between the guide conduits 65 and thedistribution tray 45, which pre-distribution tray 80 is provided with anoverflow weir 85 at its perimeter and a plurality of openings 90 nearthe perimeter.

During normal operation, liquid descending from the upper reaction bed15 collects on the collecting tray 20 where it accumulates to form alayer of liquid that covers the liquid passages 40 so that flow of gasthrough them is precluded. The flow of gas into a lower portion of thereactor 1 is via a swirler 100 closed at its top by the cover 55. Theswirler is provided with vertical vane members 95 and with horizontalgas passages 105 between the vane members 95. Gas descending from theupper reaction bed 15 is deflected off by the cover 55 and flows firstradially outwards and then radially inwards towards the horizontal gaspassages 105 of the swirler 100. On entering the horizontal gaspassages, the vane members 95 arranged alongside the horizontal gaspassages 105 impart a swirling motion to the gas which is only able tomove downwardly through the central gas passage 30 into the mixingchamber 60 below. The swirling motion imparted results in that, at thelower side of the collecting tray 20, the gas leaves the central gaspassage 30 as a swirl 108 swirling in a swirl direction 107 around avertical swirl axis 106. The swirling direction 107 is defined by thevane members 95, and can be in the swirl direction 107 as indicated inFIG. 1 or in the opposite direction. The swirling motion of the gaspromotes gas-gas interactions and thus equilibration of the gas phase.

The liquid on the collecting tray 20 passes through the liquid passages40 and into and through the guide conduits 65. For the purposes ofclarity only two guide conduits 65 and corresponding liquid passages 40are shown in FIG. 1. The injection nozzles 75 at the second ends 76 ofthe guide conduits 65 are so positioned that, during normal operation,liquid streams emerging from the injection nozzles 75 are injected, at alocation below the collecting tray 20, into the swirl 108 of gas comingfrom the central gas passage 30.

Liquid from the guide conduits 65 accumulates on the pre-distributiontray 80 where it passes downwardly to the distribution tray 45 beneaththrough the openings 90 or, sometimes, by breaching the overflow weir85. The vertical distance (X) between the collecting tray 20 and thepre-distribution tray 80, and the vertical distance (Y) between thepre-distribution tray 80 and the distribution tray 45 are preferablyrelated such that X/Y is in the range from 1 to 3. Gas is deflected bythe pre-distribution tray 80 and flows to the distribution tray 45.

The distribution tray 45 serves two purposes. Firstly, it evenlydistributes liquid and gas before the fluids enter a lower reaction bed115 and, secondly, it allows contact between liquid and gas to provideliquid-gas interaction.

The distribution tray 45 comprises a substantially horizontal plate 110with a large number of tubular downcomers 50 to provide many points ofdistribution of liquid and gas over the lower reaction bed 115. Eachdowncomer 50 comprises an upstanding (substantially vertical),open-ended tube which extends through an opening in the plate 110. Eachtube has an aperture 120 (or apertures) in its side for entry of liquidinto the tube which aperture 120 is positioned below the top surface ofthe pool of liquid which forms on plate 110 during normal operation. Thetotal number and size of the apertures 120 will be selected according tothe desired flow rate. Gas enters the top of the downcomer 50 and passesthrough it down to the lower reaction bed 115. In the downcomers 50intimate mixing between gas and liquid phases occurs.

The distributor device further comprises means for distributing a quenchfluid. These means comprise a quench ring 125 provided with ejectionnozzles 130. The quench ring 125 is located between the support grid 10and the collecting tray 20.

During normal operation, quench fluid can be emitted into the reactorthrough ejection nozzles 130 of the quench ring 125 where it comes intocontact with liquid and gas descending from the upper reaction bed 15.The quench fluid may be a reactant (e.g. hydrogen gas in a hydrotreatingor hydrocracking process), a product of the process or an inertmaterial.

Prior to more specifically discussing details of the invention, we willfirst discuss FIG. 2 in order to explain some general mathematicalbackground used to define the invention.

Physical entities like forces, movements, speeds, directions etceteracan, in a 3D (three dimensional) environment, be expressed as a vector,like direction vector D in FIG. 2. Such a 3D-vector can be decomposedinto vector components, one vector component for each dimension of the3D environment. So vector D is represented in so to say three vectorcomponents. The sum of these tree vector components then is vector D. A3D environment can as such be created in several manners. A mannerfrequently used is the 3D environment defined by an orthogonal set ofthree vector components. In such an orthogonal set of three vectorcomponents, each vector component extends perpendicular with respect toboth other vector components. Doing so with the direction vector D inFIG. 2, this direction vector D can be decomposed into a first vectorcomponent R, a second vector component A perpendicular to vectorcomponent R, and a third vector component T perpendicular to both thevector component R and vector component A.

For the purpose of defining the present invention, the vector componentsR, T and A are related to the swirling motion of gas in the mixingchamber 60. This results in:

-   -   a radial vector component R—called in claim 1 the radial        ejection vector—extending from the beginning of vector D to the        swirl axis 106 and being perpendicular to the swirl axis 106;    -   an axial vector component A—called in claim 1 the axial ejection        vector—extending parallel to the swirl axis 106 and        perpendicular to the radial vector component R;    -   a tangential vector component T—called in claim 1 the tangential        ejection vector—extending in tangential direction of the swirl        and perpendicular to both the radial vector component R and the        axial vector component A.

Further referring to FIG. 2 and claim 1: the circle 200 represents veryschematically the surface opening of a nozzle (which surface has anormal vector perpendicular to said surface which coincides with thearrow D) and arrow D represents the direction of the fluid stream—calledin claim 1 the ejection direction—emerging from the nozzle 200. In FIG.2 also the swirl direction 107 has been indicated as a circular arrowaround swirl axis 106. As one can see in FIG. 2, the tangential ejectionvector is directed opposite to the swirl direction 107. The ejectiondirection D thus is partly opposite to the swirl directionand—neglecting axial movement in the swirl and centrifugal effects inthe swirl—the tangential ejection vector is opposite the swirldirection. Viewed at the location of the nozzle 200, this tangentialejection vector T thus is so to say counter-flow to the swirl at thelocation of the nozzle 200.

Now, more detailed turning to the invention, FIG. 3 shows a view,according to arrows III of FIG. 1, onto the collecting tray 20. Thisview shows the circular quench ring 125, the ejection nozzles 130, theswirler 100 with vanes 95 determining the swirl direction 107, thedirection 150 of streams emerging from the ejection nozzles 130 (whichdirection is called the ‘ejection direction’ 150, compare also arrow Din FIG. 2), the radial component 151 of the ejection direction 150(which radial component is called the ‘radial ejection vector’ 151,compare also arrow R in FIG. 2), the tangential component 152 of theejection direction 150 (which tangential component is called the‘tangential ejection vector’ 152, compare also arrow T in FIG. 2),and—viewed in the horizontal plane—the angle α of the ejection direction150 with respect to the radial ejection vector 151. Taking into account,that the ejection direction 150 is in the embodiment of FIGS. 1 and 3actually in the horizontal plane, the angle α is the same as the anglebetween the radial ejection vector 151 and the actual ejection direction150 (note: the so called axial ejection vector—compare arrow A in FIG.2—is in this case absent as it has a value zero due to the ejectiondirection being in the horizontal plane (which is the plane defined bythe radial and tangential ejection vectors 150, 151, R, T).

As mentioned before, applicant found that directing the ejectiondirection 150 of the ejection nozzles 130 at least partly opposite theswirl direction, results in:

-   -   viewed in a horizontal plane, an improved homogeneity of the        temperature across the swirl; and    -   a reduction of the standard deviation of the temperature of the        fluid across the reactor at the (horizontal) level of the        horizontal distribution tray 45 where the fluid enters the bed        115 following the distributor device 2 (which standard deviation        will be called the ‘exit standard deviation’).

With a horizontal ejection direction 150 at an angle α=−20° (i.e. atleast partly in the same direction as the swirl direction) and α=20°with respect to the radial ejection vector 151 (i.e. at least partlyopposite the swirl direction), simulative calculations on a real livehydrocracker reactor—having the liquid phase switched off—show that theso called ‘exit standard deviation’ is at α=20° about 50% smaller thanat α=−20° when a gas is used as quench. Also for α=−10° and α=10°,simulative calculations show that the ‘exit standard deviation’ is atα=10° about 50% smaller than at α=−10° when a gas is used as a quench.This results in a longer use (about 1 month longer) of the reactorbefore maintenance for new catalyst replacement is necessary. The socalled ‘exit standard deviation’ appears to be reduced for α≧5° andα≦35° (thus α=[5°, 35°]), such as for α is in the range of [5°, 25°]. Anexplanation for this reduction of the ‘exit standard deviation’ when theejection direction is at least partly opposite the swirl direction,might be that due to opposite injection of the quench gas entering theswirler 100, the interactions between hot process gasses and the coldquench gasses are improved.

Taking into account that the swirl axis 106 will, in practicalembodiments, coincide with the vertical centre axis of the central gaspassage 30, the swirl axis 106 as used throughout this applicationcan—in practical embodiments—be read as ‘vertical centre axis of thecentral gas passage’.

That which is claimed is:
 1. A process, comprising: providingdistributor device for distributing liquid and gas in a multiple-beddownflow reactor; wherein the distributor device comprises: asubstantially horizontal collecting tray provided with: a central gaspassage and liquid passages around the central gas passage; a swirler,which swirler: is located above the collecting tray around the centralgas passage, and is provided with vanes defining a swirl direction andbeing arranged to impart a swirling motion to gas passing through thecentral gas passage so that the gas leaves the central gas passage as aswirl swirling in said swirl direction around a vertical swirl axis; oneor more ejection nozzles located above the collecting tray and arrangedfor ejecting, in an ejecting direction, a quench fluid into the gasbefore said gas enters the swirler; wherein the ejection direction isrepresented in an orthogonal set of three ejection vectors comprised ofa radial ejection vector extending perpendicular to the swirl axis, anaxial ejection vector (A) extending parallel to the swirl axis and atangential ejection vector extending tangentially with respect to theswirl axis; introducing the quench fluid through the one or moreinjection nozzle; and passing the gas through the swirler;characterized, in that the ejection nozzle is directed such that thetangential ejection vector, T) of the ejection direction of the ejectedquench fluid is directed opposite to the swirl direction.
 2. A processaccording to claim 1, further comprising using the distribution devicein hydrocarbon processing, such as hydrocracking, such as inhydrotreating and/or hydrocracking process.
 3. A distributing method fordistributing a liquid and gas in a multiple-bed downflow reactor, suchas a hydrocarbon processing reactor, like a hydrocracker; wherein adistributor device is used, which distributor device comprises asubstantially horizontal collecting tray provided with a central gaspassage; wherein gas passing in downward direction through a swirlersurrounding the central gas passage is forced into a swirling motionhaving a swirl direction around a vertical swirl axis so that the gasleaves the central gas passage as a swirl; wherein liquid is collectedon the collecting tray; wherein, at a location above the collecting trayand before the gas enters the swirler, a quench fluid, like a gaseousquench fluid, is ejected into said gas in an ejection direction, whichis, viewed in a horizontal plane, at least partly opposite to the swirldirection.
 4. The distributing method according to claim 3, wherein theejection direction is represented in an orthogonal set of three ejectionvectors comprised of a radial ejection vector extending perpendicular tothe swirl axis, an axial ejection vector (A) extending parallel to theswirl axis and a tangential ejection vector extending tangentially withrespect to the swirl axis; and wherein the ejection nozzle is directedsuch that the tangential ejection vector is directed opposite to theswirl direction.
 5. The distributing method according to claim 4,wherein the radial ejection vector is directed to the swirl axis.
 6. Thedistributing method according to claim 4, wherein the ejection directionand associated radial ejection vector define, viewed in a horizontalplane, an angle (α) in the range of from 5° to 35°.
 7. The processaccording to claim 1, wherein the ejection nozzle is directed such thatthe radial ejection vector of the ejection direction of the quench fluidis directed to the swirl axis.
 8. The process according to claim 1,wherein the ejection direction and associated radial ejection vector ofa said nozzle define an angle of more than 5°.
 9. The process accordingto claim 1, wherein the ejection direction and associated radialejection vector of a said ejection nozzle define an angle of at least10°.
 10. The process according to claim 1, wherein the ejectiondirection and associated radial ejection vector of a said ejectionnozzle define an angle of at most 35°.
 11. The process according toclaim 1, wherein the ejection direction and associated radial ejectionvector of a said ejection nozzle define an angle of at most 30°.
 12. Theprocess according to claim 1, wherein the ejection direction andassociated radial ejection vector of a said ejection nozzle define anangle in the range of from 5° to 35°.
 13. The process according to claim1, wherein: the distributor device further comprises a mixing chamberdefined between the collecting tray and the distribution tray; thecentral gas passage is surrounded by a weir; the distributor devicefurther comprises a cover located above the central gas passage andcovering the entire central gas passage; and/or the distributor devicefurther comprises a substantially horizontal pre-distribution trayarranged below the central gas passage, above the distribution tray and,in case present, lower than the optional injection nozzles of theoptional one or more guide conduits, which pre-distribution tray isprovided with an overflow weir at its perimeter and a plurality ofopenings near the perimeter; and/or one or more guide conduits arrangedbelow the collecting tray (20), wherein the guide conduits have: firstends communicating with the liquid passages (40) of the collecting trayfor receiving liquid; and second ends provided with an injection nozzlearranged to inject, in an injection direction, liquid received by thefirst ends into said swirl; wherein optionally the one or more guideconduits comprise at least eight guide conduits distributed around thecentral gas passage; and/or the injection nozzles of the one or moreguide conduits are arranged to lie within the same horizontal plane;and/or the distributor device further comprises a substantiallyhorizontal distribution tray located below the collecting tray, whichdistribution tray is provided with a plurality of downcomers fordownward flow of liquid and gas; each downcomer optionally comprising anupstanding, open ended tube having an aperture at its side for entry ofliquid into the tube; and/or the one or more ejection nozzles comprise aplurality of ejection nozzles arranged around the swirl axis to liewithin the same horizontal plane.